Carbon ion pump for removal of carbon dioxide from combustion gas and other gas mixtures

ABSTRACT

A novel method and system of separating carbon dioxide from flue gas is introduced. Instead of relying on large temperature or pressure changes to remove carbon dioxide from a solvent used to absorb it from flue gas, the ion pump method, as disclosed herein, dramatically increases the concentration of dissolved carbonate ion in solution. This increases the overlying vapor pressure of carbon dioxide gas, permitting carbon dioxide to be removed from the downstream side of the ion pump as a pure gas. The ion pumping may be obtained from reverse osmosis, electrodialysis, thermal desalination methods, or an ion pump system having an oscillating flow in synchronization with an induced electric field.

RELATED APPLICATION

This application claims the benefits of U.S. Provisional Application No.60/761,564, filed Jan. 23, 2006, and entitled, “CARBON ION PUMP FORREMOVAL OF CARBON DIOXIDE FROM COMBUSTION GAS AND OTHER GAS MIXTURES,”which is incorporated herein by reference in its entirety.

The United States Government has rights in this invention pursuant toContract No. W-7405-ENG-48 between the United States Department ofEnergy and the University of California for the operation of LawrenceLivermore National Laboratory.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates to a separation method andapparatus/system for cleaning of combustion gas followed by the captureand sequestering of carbon dioxide, and more particularly, the presentinvention relates to a water based separation method andapparatus/system for capturing and sequestering carbon dioxide fromcombustion gas and other mixtures.

2. Description of Related Art

A major limitation to reducing greenhouse gases in the atmosphere is theexpense of stripping carbon dioxide from other combustion gases. Withouta cost-effective means of accomplishing this, the world's hydrocarbonresources, if used, will continue to contribute carbon dioxide to theatmosphere.

A few major power plants around the world currently remove carbondioxide from flue gas, for sale as an industrial product. Oil companiescommonly remove carbon dioxide from natural gas to improve its energycontent. In both cases the most common technology is temperature-swingabsorption (TSA) using a methylated ethyl amine solvent (MEA).

The MEA process relies on the strongly selective bonding of carbondioxide to the solvent for selective removal from the flue gas, butrequires considerable heating to increase the gas pressure in theremoval step to an acceptable level. In particular, the flue gascontacts the MEA dissolved in water in a packed column, and then thecarbonated solution is heated to 120° C. to extract a nearly pure carbondioxide gas. Sulfur and nitrous oxide are removed ahead of this stepbecause they bind so tightly to the solvent that they cannot be removed.An alternative MEA cycle using pressure cycling can be used in somecases, when the inlet gas to be separated is at high pressure and thecarbon dioxide can be removed from the solvent by lowering the ambientpressure. In both this process and the temperature swing process, thecarbon dioxide fugacity is changed by changing the physical conditionsof the solvent. This is inefficient due to the energy unrecoverably lostdoing work on a large volume of solvent, in addition to the mechanicallycomplex system and the need for frequent solvent addition due todegradation. It is a fundamentally complex and chemically-intensiveprocess only suitable for large-scale industrial separation today and itis too expensive to contribute a globally-large removal of carbon fromcombustion sources.

The Greenhouse Gas Program of the International Energy Agency (Davisonet al. 2001) has studied the application of this technology to electricpower plants. They estimate an energy cost of approximately 35% of thepower generated by a pulverized coal power plant is required for thistype of carbon dioxide removal. Many variants are under study, whichpermit slightly higher efficiency or longer solvent life, includingsolid sorbents; thus far, dramatic improvements have not been seen.

Accordingly, a need exists for an improved process and system to controlthe removal of CO₂ in an economical and environmentally safe way. Thepresent invention is directed to such a need.

SUMMARY OF THE INVENTION

The present invention is directed to a Carbon ion pumping process forextracting and sequestering CO₂ that includes: dissolving apredetermined gas into a water wash, wherein the water wash includes adegree of alkalinity; passing the water having the dissolved gas into ameans configured to produce a predetermined ionic concentrate; andharvesting a resultant CO₂.

Another aspect of the present invention is directed to a Carbon ionpumping process for extracting and sequestering CO₂ that includes:dissolving a predetermined gas into water, wherein the water comprises adegree of alkalinity; directing the water through a first channel and asecond channel; oscillating a fluid flow therethrough a plurality offlow channels so as to fluidly communicate the first channel with thesecond channel; applying a periodic electric field about each of theplurality of flow channels in synchronization with the oscillating fluidflow so as to enable a directed movement of predetermined ions from thefirst channel to the second channel so as to produce an ionicconcentrate in the second channel; and extracting and sequesteringCarbon Dioxide (CO₂) from the second channel.

Another aspect of the present invention is directed to a system forremoving and sequestering a predetermined amount of Carbon Dioxide (CO₂)from a gas that includes: a distribution means for introducing apredetermined gas; a water wash configured to produce an ionic solution,wherein the water wash is operably coupled to the distribution means;and a means operably coupled to the water wash and configured to producean ionic concentrate in the ionic solution, wherein the carbon dioxidecan be extracted and sequestered as a pure gas by increasing theoverlying vapor pressure within the ionic solution.

A final aspect of the present invention is directed to a system forremoving and sequestering a predetermined amount of Carbon Dioxide (CO₂)from a gas that includes: a distribution means for introducing apredetermined gas; a water wash having a degree of salinity so as toproduce an ionic solution, wherein the water wash is operably coupled tothe distribution means; a feed flow channel operably coupled to thewater wash; a concentrate flow channel also operably coupled to thewater wash; a plurality of flow channels configured to fluidlycommunicate an oscillating flow between the feed flow channel and theconcentrate flow channel; and one or more pairs of conductive platesadapted about the plurality of flow channels, wherein an appliedperiodic electric field to the one or more pairs of conductive plates insynchronization with the oscillating flow facilitates a directedmovement of predetermined ions therethrough said flow channels from thefeed flow channel to the concentrate flow channel; and wherein aresultant overlying vapor pressure produced in the ionic concentrateenables the carbon dioxide to be extracted and sequestered as a puregas.

Accordingly, the present system and method approach to increasing theconcentration of the extracted gas permits new approaches to treatingflue gas and other gas mixtures of inert gas like nitrogen, with acidgases like carbon dioxide or sulfur dioxide, since the slightly basicwater used as the extraction medium is impervious to trace acid gasesthat destroy existing solvents, and no pre-separation is necessary. Theprocess may be operated in such a way to produce clean water (similar toreverse osmosis water) as an additional product.

BRIEF DESCRIPTION OF THE DRAWINGS

The accompanying drawings, which are incorporated into and form a partof the disclosure, illustrate an embodiment of the invention and,together with the description, serve to explain the principles of theinvention.

FIG. 1 is a general illustration of the Carbon ion pump apparatus of thepresent invention.

FIG. 2 is a general illustration of the preferred Carbon ion pumpapparatus of the present invention.

FIG. 3 shows a model indicating the effects of the ion pumping processfor a simple sodium bicarbonate-phosphate water system of the presentinvention.

FIG. 4 a illustrates the oscillatory back and forth fluid movement andthe ratcheting of ions across flow channels.

FIG. 4 b illustrates the oscillatory back and forth fluid movement andthe ratcheting of ions across flow channels.

FIG. 4 c illustrates the oscillatory back and forth fluid movement andthe ratcheting of ions across flow channels.

FIG. 5 a shows the movement of cations and anions with the e-field off.

FIG. 5 b shows the movement of cations and anions with the e-field on.

DETAILED DESCRIPTION OF THE INVENTION

Referring now to the drawings, specific embodiments of the invention areshown. The detailed description of the specific embodiments, togetherwith the general description of the invention, serves to explain theprinciples of the invention.

Unless otherwise indicated, all numbers expressing quantities ofingredients, constituents, reaction conditions and so forth used in thespecification and claims are to be understood as being modified in allinstances by the term “about”. Accordingly, unless indicated to thecontrary, the numerical parameters set forth in the specification andattached claims are approximations that may vary depending upon thedesired properties sought to be obtained by the subject matter presentedherein. At the very least, and not as an attempt to limit theapplication of the doctrine of equivalents to the scope of the claims,each numerical parameter should at least be construed in light of thenumber of reported significant digits and by applying ordinary roundingtechniques. Notwithstanding that the numerical ranges and parameterssetting forth the broad scope of the subject matter presented herein areapproximations, the numerical values set forth in the specific examplesare reported as precisely as possible. Any numerical value, however,inherently contains certain errors necessarily resulting from thestandard deviation found in their respective testing measurements.

Moreover, in the description of the invention herein, it is understoodthat a word appearing in the singular encompasses its pluralcounterpart, and a word appearing in the plural encompasses its singularcounterpart, unless implicitly or explicitly understood or statedotherwise. Furthermore, it is understood that for any given component orembodiment described herein, any of the possible candidates oralternatives listed for that component may generally be usedindividually or in combination with one another, unless implicitly orexplicitly understood or stated otherwise. Additionally, it will beunderstood that any list of such candidates or alternatives is merelyillustrative, not limiting, unless implicitly or explicitly understoodor stated otherwise.

Finally, various terms used herein are described to facilitate anunderstanding of the invention. It is understood that a correspondingdescription of these various terms applies to corresponding linguisticor grammatical variations or forms of these various terms. It will alsobe understood that the invention is not limited to the terminology usedherein, or the descriptions thereof, for the description of particularembodiments.

General Description

Carbon dioxide makes up from 5% (modern gas-fired plants) to 19% (moderncoal plants) of the flue gas from a power plant. The remainder is mostlynitrogen, unused oxygen, and oxides of nitrogen and sulfur (which arestrong greenhouse gases in addition to contributing to poor quality).

As disclosed herein, use of a liquid absorber to separate gases dependson both selective absorption of the desired gas, and changing the vaporpressure (properly the fugacity) of the gas over the solvent. Carbondioxide makes up from 5% (modern gas-fired plants) to 19% (modern coalplants) of the flue gas from a power plant. The remainder is mainlynitrogen, unused oxygen, and oxides of nitrogen and sulfur (which arestrong greenhouse gases in addition to contributing to poor airquality). Carbon dioxide, in particular, is soluble in water, in whichit spontaneously interconverts between CO₂ and H₂CO₃ (carbonic acid).The relative concentrations of CO₂, H₂CO₃, and the deprotonated formsHCO₃ ⁻ (bicarbonate) and CO₃ ²⁻ (carbonate) depend on pH. In neutral orslightly alkaline water (pH of greater than 6.0), the bicarbonate formpredominates (>50%) becoming the most prevalent (>95%) at the pH ofseawater.

The present invention thus provides for a water based method and systemfor separating carbon dioxide from flue gas and other combustion gasesbased on ionic pumping of carbonate ions dissolved in the fluid. Insteadof relying on large temperature or pressure changes to remove carbondioxide from solvent used to absorb it from, for example flue gas (e.g.,CO₂, H₂O, N₂, SO_(x), NO_(x)), the ion pumping methods and systems whenconfigured to receive the dissolved carbonate ions, dramaticallyincreases the concentration of such ions in solution.

The ion pumps, as disclosed herein, can be configured from known systemsunderstood by those of ordinary skill in the art, such as, but notlimited to, membrane process (e.g., electro dialysis and reverse osmosispumps), or any of the available thermal processes (e.g., Multiple-effectevaporation/distillation (MED), Multi-stage flashevaporation/distillation (MSF), Vapor compression distillation (LTV),and Solar distillation).

A preferred ion pump configuration, as discussed herein, includesrelated architecture disclosed in Incorporated by reference Co-pending,Co-filed U.S. application Ser. No. ______ titled “Deionization andDesalination Using Electrostatic Ion Pumping” by Bourcier et al., thedisclosure of which is herein incorporated by reference in its entirety.In such a structure, as discussed in the Co-pending and Co-filedapplication, externally applied electrostatic fields in conjunction withan oscillating fluid flow immobilize and separate the Carbonate ionsfrom the received fluids. The desired ions are held in place duringfluid movement in one direction, and released for transport during fluidmovement in the opposite direction. The targeted ions are “ratcheted”across the charged surface from the feed side to the concentrate side.Such a method and system is very simple and involves only pumps, chargedsurfaces, and manifolds for fluid collection. It is therefore operatorfriendly, and amenable to remote operation.

The charged ion collection surfaces are often in a substantiallyparallel configuration or even in a spiral-wound configuration all ofwhich are designed to facilitate both cleaning and swapping ofreplacements for damaged modules. The surfaces themselves can bemetalized electrodes or thin sheets of carbon aerogel composites, ornano-engineered conductive surfaces of various geometries and surfaceareas, such as, but not limited to, ion-track-etched polycarbonates withmetalized surfaces to enable desired sorptive surface morphology andpore structures. As another beneficial electrode structure, beds ofcarbon aerogel particles can alternatively be used to form electrodesbecause such beds of carbon aerogel particles have much higher specificarea and sorption capacity than beds of conventional carbon powder, andtherefore are superior electrodes for deionization purposes.

Whichever ion pump system and method that is chosen to receive thedissolved carbonate ions, it is to be appreciated that such ion pumpconfigurations nonetheless increase the overlying vapor pressure ofcarbon dioxide gas, which can then be removed by the novel system of thepresent invention from the downstream side of the ion pump as a puregas. Such novel embodiments of the present invention to increasing theconcentration of the extracted gas permits new approaches to treatingflue gas, since the slightly basic water used as the extraction mediumis impervious to trace acid gases that destroy existing solvents, and nopre-separation is necessary.

Specific Description

FIG. 1 shows a general layout of the Carbon ion pumping embodiment ofthe present invention, and is generally designated as reference numeral10. As shown in FIG. 1, Carbon ion pumping system/apparatus 10 caninclude, a source of flue gas (e.g., CO₂, H₂O, N₂, SO_(x), NO_(x))and/or other gas mixtures 1, a water wash 2, a water basin and deliverysystem 4 having an introduced buffer pH (e.g., phosphate), and a Carbonion pump 5. The system/process 10 is thus designed to dissolve flue gas(e.g., CO₂, H₂O, N₂, SO_(x), NO_(x)) and/or other gas mixtures first inslightly alkaline water as introduced by the water wash 2 prior toproducing a concentrate from which a harvested CO₂ can be produced.

Table 1 below shows the dissolution of common flue and combustion gasesin addition to concentration factors of the present invention.

TABLE 1 How acid flue gas components readily dissolve and ionize inbuffered water. Coal Flue Gas Dissolved Concentration ProportionConcentration Factor 13.9% CO₂ + H₂O

1200 ppm  (300X relative H⁺ + HCO₃ ⁻ to Nitrogen) 0.07% SO_(x) + H₂O

(all of it) (Substantially Large) H⁺ + HSO₄ ⁻ 0.02% NO_(x) + ~H₂O

(all of it) (Substantially Large) H⁺ + HNO₃ ⁻ 73.8% N₂ + H₂O

13 ppm N₂ + H₂O  3.0% O₂ + H₂O

 3 ppm O₂ + H₂O

Returning to FIG. 1, the water wash 2 system itself can be incorporatedfrom known systems utilized by those of ordinary skill in the art. As anillustration only, the common system can include a plurality of spraylevels to inject the liquid so as to contact the flue gas, which isdesigned to flow through such a water wash 2 system at a predeterminedconstant velocity. The number of spray levels can be varied depending onthe effective liquid to gas (L/G) ratios. In addition, spray nozzles ofdifferent sizes producing different flow rates, spray patterns, anddroplet sizes can also be utilized. The water having the flue gas thenpasses from water wash 2 to water basin 4 having an introduced buffer pH(e.g., phosphate) to increase CO₂ carrying capacity upon recycling.

Water basin 4 is also coupled to operating pumps and/or operating valves(not shown) known and understood by those of ordinary skill in the artto receive recycled fluids (not shown) from ion pump 5 in addition todirecting flow to ion pump 5, so as enable the harvesting of a desiredgas, such as CO₂ 6, as shown in FIG. 1.

Upon receiving the dissolved ions in a fluid having a pH of greater thanabout 6.5 so as to increase CO₂ carrying capacity, the ion pump 5 canproduce a concentrate from which carbon dioxide 6 is released. Theconcentrate (not shown) is recombined with a dilute stream (not shown)from the ion pump 5 and re-cycled to the water wash 4. In addition,nitrate and sulfate are also concentrated with the bicarbonate andremoved separately as solids (they are more stable in solution than thecarbonate).

FIG. 2 shows a preferred Carbon ion pumping embodiment of the presentinvention, and is generally designated as reference numeral 20, whereinlike reference numerals are used when common to the system 10, as shownin FIG. 1. As shown in FIG. 2, Carbon ion pumping system/apparatus 20,similar to system 10 as shown in FIG. 1, can include a source of fluegas (e.g., CO₂, H₂O, N₂, SO_(x), NO_(x)) and/or other gas mixtures 1, awater wash 2, a water basin and delivery system 4 having an introducedbuffer pH (e.g., phosphate to increase CO₂ carrying capacity) and aCarbon ion pump designated as reference numeral 5′ (also shown withinthe dashed box). As discussed above, ion pump 5′ and relatedarchitecture is discussed in Incorporated by reference Co-pending,Co-filed U.S. application Ser. No. ______ titled “Deionization andDesalination Using Electrostatic Ion Pumping” by Bourcier et al.

As described above, upon receiving the dissolved ions in a fluid havinga pH of greater than about 6.5 (such a pH increases CO₂ carryingcapacity) the ion pump 5′, as shown in FIG. 2, can produce a concentrate28 from which carbon dioxide 6 is released. Concentrate 28 (as shown byan accompanying directional arrow) is recombined with a dilute stream 18(also shown by an accompanying directional arrow) often having aresultant pH of about 6.0, from the ion pump 5 and re-cycled to thewater wash 4. In addition, nitrate and sulfate 32 are also concentratedwith the bicarbonate concentrate 28 and either removed separately assolids or evolved in gas form (they are more stable in solution than thecarbonate) by methods known and understood by those of ordinary skill inthe art.

With respect to the ion pump 5′, such an apparatus is designed with afeed fluid flow channel 12 (fluid flow shown as a one-way directionalarrow) and a concentrate fluid flow channel 14 (fluid flow also shown asa one-way directional arrow), that fluidly communicate with a pluralityof disposed fluid flow channels 8 (three are referenced for simplicity),and a plurality of spaced-apart, often equidistantly spaced apart,engineered corrosion resistant charge collection surfaces 16, such asbut not limited to metalized electrodes, ion track etched polycarbonateswith metalized surfaces, and/or carbon aerogel electrodes.

In the method of operation, a slightly alkaline fluid having a pH ofgreater than about 6.5 and having desired dissolved ions that originatefrom a source, such as, but not limited to, (e.g., CO₂, H₂O, N₂, SO_(x),NO_(x)) and/or other gas mixtures can be received by feed fluid flowchannel 12 and concentrate fluid flow channel 14 and can be directedback and forth in an oscillating manner between the plurality of flowchannels 8, e.g., as illustrated by the double directional arrow in FIG.1.

An applied e-field is synchronized with an oscillation fluid pumpingfrequency by applying the electric field at predetermined times to thedesigned flow speeds in the feed fluid flow channel 12 and concentratefluid flow channel 14 in a predetermined manner using, for example, acomputer 7. As an illustration, the fluid flow rates can be manipulatedby a computer (not shown) controlled fluid circuit (e.g., feed pumps andconcentrate pump, and/or operating valves, operably coupled to basin anddelivery system 4) in synchronization with applied e-fields directed bythe same computer through a coupled electrical circuit (not shown). Seea similar discussion of this operation in Incorporated by referenceCo-pending, Co-filed U.S. application Ser. No. ______ titled“Deionization and Desalination Using Electrostatic Ion Pumping” byBourcier et al. Such controls can be made via the computer either viaoperator control or automatically using custom and/or commercialsoftware (e.g., via a graphical computer interface software program,such as, for example, LabVIEW).

The flow channels 8 themselves are arranged to have widths between about0.1 mm and up to about 2 mm, often up to about 0.5 mm and lengthsbetween about 0.1 mm and up to about 10 cm in a configured manner thatis based upon the positioning of the separated charge collectionsurfaces 16 operating as conductors, such that when a voltage betweenabout 0.1 volts and up to about 10 volts is applied to the chargecollection surfaces 16, predetermined ions, such as disassociated ionsfrom flue gas, are attracted and electrosorb to their surfaces; cationsto negatively charged collection surfaces, and anions to positivelycharged collection surfaces.

The ion content, e.g., the HCO₃ ⁻ concentration, of the moving fluid isreduced by the amount of sorbed ions removed from bulk solution (i.e.,from feed fluid flow channel 12). The ions do not flow with the fluid;they remain attached to the electrode surface in the electrostaticdouble layer. If the fluid now flows in the reverse direction, andsimultaneously the voltage is removed, the ions return to solution andare transported with the solution. As the solution moves back and forthbetween the charge collection surfaces 16 via the plurality of flowchannels 8, the desired ions will be “ratcheted” across the platesurfaces so as to be directed along a concentrate flow channel line. Theion pump effectively increases the concentration of the bicarbonate (redline) with a corresponding increase in carbon dioxide pressure. Thecarbon dioxide 6 is released at a pressure of about one bar. The ionpump increases the HCO₃ ⁻ concentration; for flue gas from a coal-firedpower plant, an increase of 30 will release about 6.5 grams of purecarbon dioxide per liter of fluid.

Specifically, if feed source fluid is received from basin and deliverysystem 4 within feed fluid flow channel 12 is provided on one side ofthe charge collection surfaces 16, substantially perpendicular to suchsurfaces (as shown in FIG. 2), the ions, e.g., HCO₃ ⁻ , by passing it bya series, i.e., a plurality of substantially parallel charge collectionsurfaces 16 and the water 18 cleaned by such a method can also beharvested via a feed fluid output channel (shown at the top of feed flowchannel 12).

The ions, such as HCO₃ ⁻ , passes along the charge collection surfaces16 and is accumulated in the concentrate fluid flow channel 14collecting on the side opposite to the feed fluid flow channel 12. Theconcentrate that does not come off as carbon dioxide 6 is thus recycledvia a waste output channel 28 (denoted as a carbonate phosphatesolution) and combined with the cleaned water 18 output and furtherdirected to water basin and delivery system 4. The greater the number ofcharge collection surfaces 16, and thus the greater the number of flowchannels 8, the greater the amount of ions, such as HCO₃ ⁻ , that isremoved. The greater the number of ions attached to the chargecollection surfaces 16, the fewer the number of charge collectionsurfaces 16 and the fewer the number of flow channels 8 are needed for adesired amount of ion removal. It is to be appreciated that such aparallel flow arrangement, as shown in FIG. 1, enables thesystem/apparatus to perform in the event that any or a number of theflow channels 8/charge collection surfaces 16 become inoperable for anyparticular reason, e.g., by fouling, electrical non-communication,plugging, etc.

FIG. 3 shows a model indicating the effects of the ion pumping process,as disclosed herein, for a simple sodium bicarbonate-phosphate watersystem. The ion pump effectively increases the concentration ofbicarbonate (shown as reference numeral 40 attached to a directionalarrow) with a corresponding increase in carbon dioxide pressure. Carbondioxide is thus released at a pressure of about one bar. The ion pumpincreases the HCO₃ ⁻ concentration. For flue gas from a coal-fired powerplant, an increase of 30 releases about 6.5 grams of pure carbon dioxideper liter of fluid.

FIGS. 4 a-c shows schematically what happens to an individual packet ofelectrolyte solution (denoted by the letter S) as it travels up the feedfluid flow channel 12, as similarly shown in FIG. 2.

In particular, FIG. 4 a illustrates how the oscillatory pumping back andforth of the present invention at frequencies of greater than about 0.5Hz between the charge collection surfaces 16 causes the solution Spacket to enter the space (i.e., flow channel 8) between the surfaces16.

In FIG. 4 b, a field is applied by having predetermined chargecollection surfaces 16 enabled with a positive 22 and a negative voltage24 coupled thereto in timing with the oscillating flow rate of thechannels 12 and 14. (It is to be appreciated that while FIG. 2 billustrates a single charge collection surface having a positive charge,it is to be noted that each charge collection surface 16 can also bearranged to have opposite charges applied to a respective oppositeface).

In the arrangement of FIG. 4 b, ions, such as HCO₃ ⁻ , are sorbed to theparticular electrode charge collection surface(s) 16 because of theapplied field. When the packet S moves back out (i.e., back into feedfluid channel 12) between the charge collection surface(s) 16 because ofthe oscillating flow rate within channels 12 and 14, it has lost some ofits ions, which remains on the surface of a respective chargedcollection surface(s) 16.

FIG. 4 c illustrates how subsequent cycles force HCO₃ ⁻ to the right(denoted by the black curved arrows) and into concentrate fluid flowchannel 14. For a particular cycle, the applied field that had beeninduced, as shown in FIG. 4 b, is removed, and flow rate is increased ina timed manner in feed fluid flow channel 12 to coincide with theremoval of the applied field, and ions once immobilized by the appliedfield are thus fluidly moved in a direction towards the concentratedfluid flow channel 14. Additional cycles ratchets trapped ions furthertoward the direction of concentrate fluid flow channel 14.De-concentrated S fluid packet then moves up and the cycle is repeatedwith each charge collection surface(s) 16 stage.

FIGS. 5 a-b further illustrates the movement of a plurality of cations22 and anions 24 during the same process. Electrostatic charge (denotedby + and − in FIG. 5 b) on electrodes 16 holds cations 22 (denoted bythe darkened circles) and anions 24 (denoted by the white circles) inplace during fluid movement to the left when an e-field is applied, butreleases them for fluid movement to the right when the e-field isremoved, as shown in FIG. 5 a. Plate spacing (widths between about 0.1mm and up to about 2 mm, often up to about 0.5 mm and lengths betweenabout 0.1 mm and up to about 10 cm) is optimized to balance desirableshort path length for ion separation, with wide spacing for fluid flow.

It should be understood that the invention is not intended to be limitedto the particular forms disclosed. Rather, the invention is to cover allmodifications, equivalents, and alternatives falling within the spiritand scope of the invention as defined by the following appended claims.

1. A process for extracting and sequestering CO₂, comprising: dissolvinga predetermined gas into a water, wherein said water comprises a degreeof alkalinity to increase CO₂ carrying capacity; passing the waterhaving said dissolved gas into a means configured to produce apredetermined ionic concentrate; and extracting and sequestering aresultant CO₂.
 2. The process of claim 1, wherein said means comprisesan ion pump.
 3. The process of claim 1, wherein said means furthercomprises at least one apparatus selected from: an electro dialysisapparatus, a reverse osmosis apparatus, a Multiple-effectevaporation/distillation (MED) apparatus, a Multi-stage flashevaporation/distillation (MSF) apparatus, a Vapor compressiondistillation (LTV) apparatus, and a Solar distillation apparatus.
 4. Theapparatus of claim 1, wherein said gas comprises combustible gases. 5.The apparatus of claim 1, wherein said gas comprises at least one gasselected from: CO₂, H₂O, N₂, SO_(x), and NO_(x).
 6. The process of claim1, wherein said means is adapted to produce a vapor pressure of greaterthan about 1 bar of a predetermined ionic concentrate so as to producesaid resultant CO₂.
 7. The process of claim 1, further comprisingcombining said ionic concentrate to a diluted stream so as to berecycled into said water wash.
 8. The process of claim 1, furthercomprising adding Phosphate to said water wash to buffer the pH andproduce said alkalinity.
 9. The process of claim 8, wherein said pH isgreater than 6.0.
 10. The process of claim 1, further comprisingremoving Nitrate and Sulfate bi-products from said ionic concentrate.11. A process for extracting and sequestering CO₂, comprising:dissolving a predetermined gas into water, wherein said water comprisesa degree of alkalinity to increase CO₂ carrying capacity; directing saidwater through a first channel and a second channel; oscillating a fluidflow therethrough a plurality of flow channels so as to fluidlycommunicate said first channel with said second channel; applying aperiodic electric field about each of said plurality of flow channels insynchronization with said oscillating fluid flow so as to enable adirected movement of predetermined ions from said first channel to saidsecond channel so as to produce an ionic concentrate in said secondchannel; and extracting and sequestering Carbon Dioxide (CO₂) from saidsecond channel.
 12. The apparatus of claim 11, wherein said gascomprises combustible gases.
 13. The apparatus of claim 11, wherein saidgas comprises at least one gas selected from: CO₂, H₂O, N₂, SO_(x), andNO_(x).
 14. The process of claim 11, further comprising producing avapor pressure of greater than about 1 bar of said ionic concentrate insaid second channel to enable the extracting and sequestering of saidCO₂.
 15. The process of claim 11, further comprising combining saidionic concentrate to a diluted stream so as to be recycled into saidwater wash.
 16. The process of claim 1, further comprising addingPhosphate to said water wash to buffer the pH and produce saidalkalinity.
 17. The process of claim 16, wherein said pH is greater than6.0.
 18. The process of claim 11, further comprising removing Nitrateand Sulfate bi-products from said ionic concentrate.
 19. A system forremoving and sequestering a predetermined amount of Carbon Dioxide (CO₂)from a gas, comprising: distribution means for introducing apredetermined gas; a water wash configured to produce an ionic solution,said water wash operably coupled to said distribution means; and meansoperably coupled to said water wash and configured to produce an ionicconcentrate in said ionic solution, wherein the carbon dioxide can beextracted and sequestered as a pure gas by increasing the overlyingvapor pressure within said ionic solution.
 20. The system of claim 18,wherein said means operably coupled to said water wash comprises an ionpump.
 21. The system of claim 18, wherein said means operably coupled tosaid water wash further comprises at least one apparatus selected from:an electro dialysis apparatus, a reverse osmosis apparatus, aMultiple-effect evaporation/distillation (MED) apparatus, a Multi-stageflash evaporation/distillation (MSF) apparatus, a Vapor compressiondistillation (LTV) apparatus, and a Solar distillation apparatus. 22.The system of claim 18, wherein said gas comprises combustible gases.23. The system of claim 18, wherein said gas comprises at least one gasselected from: CO₂, H₂O, N₂, SO_(x), and NO_(x).
 24. The system of claim18, wherein said vapor pressure is greater than about 1 bar.
 25. Thesystem of claim 18, wherein said alkalinity comprises a pH greater than6.0 to increase CO₂ carrying capacity.
 26. The system of claim 18,wherein a recycling system is operably coupled to said means forproducing said ionic concentrate so as to combine said ionic concentratewith a dilute stream so as to be re-cycled in said water wash.
 27. Asystem for removing and sequestering a predetermined amount of CarbonDioxide (CO₂) from a gas, comprising: distribution means for introducinga predetermined gas; a water wash having a degree of salinity so as toproduce an ionic solution, said water wash operably coupled to saiddistribution means; a feed flow channel operably coupled to said waterwash; a concentrate flow channel operably coupled to said water wash; aplurality of flow channels configured to fluidly communicate anoscillating flow between said feed flow channel and said concentrateflow channel; and one or more pairs of conductive plates adapted aboutsaid plurality of flow channels, wherein an applied periodic electricfield to said one or more pairs of conductive plates in synchronizationwith said oscillating flow facilitates a directed movement ofpredetermined ions therethrough said flow channels from said feed flowchannel to said concentrate flow channel; and wherein a resultantoverlying vapor pressure produced in said ionic concentrate enables thecarbon dioxide to be extracted and sequestered as a pure gas.
 28. Thesystem of claim 26, wherein said applied synchronized periodic electricfield comprises a voltage from about 10 volts down to about 0.1 volts.29. The system of claim 26, wherein said applied synchronized periodelectric field comprises configuring pairs of charge collection surfacesabout said plurality of flow channels.
 30. The system of claim 28,wherein said charge collection surfaces comprise pairs of substantiallyparallel conductive electrodes.
 31. The system of claim 29, wherein saidconductive electrodes comprise conductive materials selected from:metalized electrodes, thin sheets of carbon aerogel composites, andion-track-etched polycarbonates with metalized surfaces.
 32. The systemof claim 26, wherein said oscillating flow comprises applying anoscillating pump flow of greater than about 0.5 Hz.
 33. The system ofclaim 26, wherein said predetermined gas comprises combustible gases.34. The system of claim 26, wherein said predetermined gas comprises atleast one gas selected from: CO₂, H₂O, N₂, SO_(x), and NO_(x).
 35. Thesystem of claim 26, wherein said overlying vapor pressure is greaterthan about 1 bar.
 36. The system of claim 26, wherein said alkalinitycomprises a pH greater than 6.0 to increase CO₂ carrying capacity. 37.The system of claim 26, wherein a recycling system is operably coupledto said system for producing said ionic concentrate so as to combinesaid ionic concentrate with a dilute stream so as to be re-cycled insaid water wash.